CN103201002A - In-situ vaporizer and recuperator for alternating flow device - Google Patents

In-situ vaporizer and recuperator for alternating flow device Download PDF

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CN103201002A
CN103201002A CN2011800540610A CN201180054061A CN103201002A CN 103201002 A CN103201002 A CN 103201002A CN 2011800540610 A CN2011800540610 A CN 2011800540610A CN 201180054061 A CN201180054061 A CN 201180054061A CN 103201002 A CN103201002 A CN 103201002A
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CN103201002B (en
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杰弗里·M·格伦达
弗兰克·赫什科维茨
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ExxonMobil Technology and Engineering Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
    • B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
    • B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
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    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
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    • C01—INORGANIC CHEMISTRY
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    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/46—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using discontinuously preheated non-moving solid materials, e.g. blast and run
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/14—Details thereof
    • F23K5/22—Vaporising devices
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Abstract

The present invention relates to a device for converting a liquid feed stream to a gaseous vapor stream comprising: (a) channel means having a first and second end, said channel means having a plurality of channels connecting said first and second end, said channel means having a substantially solid region and a void region, (b) inlet means for directing the liquid feed stream to the first end of the plurality of channels, and (c) outlet means for directing the gaseous vapor stream from said plurality of channels, where said channels have, at any distance d between the inlet and outlet, a geometric configuration, perpendicular to the feed flow direction; and is characterized by (1) a void area A'(x) and, (2) a channel total cross-sectional area A(x), where the void area A'(x) is a fraction of the total area A(x) and a average void fraction along a length of device L ranges from about 0.3 to about 0.95.

Description

The original position vaporizer and the recuperator that are used for the alternating current device
Technical field
The present invention relates to a kind of original position vaporizer and heat reclaim unit for the alternating current system, it can be stated from the haulage vehicle.
Background technology
The many industrial process that comprise steam reformation need convert liquid feed stream (for example gasoline or other liquid hydrocarbon or water) to vapor stream usually before chemical conversion.Conventional vaporizer and boiler need a large amount of thermal masses and usually because pressure oscillation and temperature change and perform poor under transient operation.Use for automobile, in wide dynamic operation scope the transient state necessary condition of (being called range) operation make the vapor stream difficult treatment and to the equivalent proportion between fuel and oxidant control challenge.Many application need this vaporization and mixed process to take place under accurate mass flow control, operate in big dynamic range, and original position is present in the reactor volume so that the heat transfer loss minimizes, and causes low droop loss, and the corrosion of anti-flow of process fluid.Therefore, have the needs to following technology in the prior art: this technology can provide accurate mass flow control, operates in big dynamic temperature and pressure limit, and the heat transfer loss is minimized, and causes low droop loss, and the corrosion of anti-flow of process fluid.
The invention describes the novel original position vaporizer and the heat reclaim unit that are particularly suitable for the alternating current reactor assembly, wherein through the materials flow of device the vaporizing liquid pattern with replace between the heating mode again.In a preferred embodiment, it is as in for example US patent 7,491, the part of the pressure swing reforming device described in 250 (" PSR ") system.It makes it possible to realize being disposed in the design that the small-sized synthesis gas in the haulage vehicle for example produces system.
The inventor has had been found that this kind original position vaporizer that the institute's description advantage above of realizing is required and the specific design standard of heat reclaim unit.These features comprise the technical parameter on geometry, thermal capacity and heat transfer, flow channel size and voidage and voidage gradient in order to minimize device size and weight.The unique combination of these design standards has produced as the high efficiency vaporizer/recuperator that proves in the application to pressure swing reforming, and the application of described pressure swing reforming is as instructing in patent mentioned above.
Summary of the invention
The present invention relates to a kind of for the device that liquid feed stream is converted to gas vapor stream, this device comprises: the channel component that (a) has first end and second end, described channel component has the passage of described first end of a plurality of connections and second end, described channel component has roughly zone and the void area of entity, (b) inlet member, described inlet member is used for described liquid feed stream is directed to first end of described a plurality of passages, and (c) outlet member, described outlet member is used for guiding from the gas vapor stream of described a plurality of passages, the any distance x place of wherein said passage between described import and outlet has the geometry perpendicular to described feed flow direction, it is characterized in that (1) void area A ' (x), and (2) total cross-sectional area A (x), wherein the described void area A ' as the part of described gross area A (x) (x) is
Figure BDA00003165165200021
And the average void fraction along the length L of installing is
Figure BDA00003165165200022
Wherein said average void fraction is about 0.3 to about 0.95.
In one embodiment, described voidage is along the length of described device and change.
In another embodiment, estimate that the mean change of described voidage is about 0.01 to about 0.5 on the total length of this device.
In another embodiment of the invention, this device has continuously constant voidage zone, and described zone changes along the length of this device.
Description of drawings
Fig. 1 herein is the schematic diagram of embodiment of the present invention.
The specific embodiment
The present invention relates to change into for the one or more liquid flow that will supply the device of gas vapor stream.More specifically, the device that the present invention relates to move in cyclic process relies on this cyclic process, liquid hydrocarbon and randomly aqueous mixtures be converted into hydrocarbon steam and steam mixture randomly.Are purposes in pressure oscillating steam reformation process for an application-specific of the vaporization of liquid hydrocarbon and current.
This device is designed to the continuous operation by two phase process that circulate.Phase I is the vaporization pattern, and second stage is again heating mode.We have found that the specific design standard or the feature that produce following original position vaporizer and heat reclaim unit, it can realize big dynamic operation scope, minimum pressure drop, corrosion-resistant and use miniaturization fully and lighting for mobile.These features are included in vaporizer interior geometry, thermal capacity and heat-transfer capability, flow channel size and voidage and the technical parameter on the voidage gradient.
Device of the present invention is made of the partially porous medium with the interstitial channels that comprises a stack features size and dimension.Void area in device forms one group of path that connects, and fluid (with liquid state or gaseous state) can pass through this device by described path.For example, notional device geometry of simplifying shown in Fig. 1.Voidage or fractional porosity are the unlimited marks of the volume that device is stated in the set point place in the space.Fluid can access to plant arbitrary end, and leave in the opposite end.First purpose of this device is to make the liquid stream of supply be vaporized into steam.As shown in fig. 1, liquid stream to be vaporized will will be restricted to the inlet surface that is labeled as (10) herein by the surface of its access to plant (11).The materials flow of vaporization is restricted to exit surface (12) by its surface of leaving.In the heating period again of device, high temperature adds hot-fluid again and can enter by the import or export surface, and leaves in corresponding opposite end.In the schematic diagram shown in Fig. 1, add hot-fluid again and be shown as and vaporization flow (16) counter-current flow.Adding hot-fluid (14) again is shown in Figure 1 for and enters exit list surface current (12) and locate to leave as materials flow (15) in inlet surface (10).In Fig. 1, described device is shown as the cylindrical appliance with constant cross-sectional area.In fact, the device shape of cross section is not limited to cylindrical, and can be rectangle, square, triangle or other shape.Described cross-sectional area also can change with axial location.
General provision have two cycles of operation or the stage of described device, and these has limited design feature of the present invention.At t running time VaporizationPeriod 1 in, liquid or mixtures of liquids or the materials flow (16) that comprises liquid are sentenced given volume of liquid flow rate Q in import (10) LiquidEnter described device.This liquid stream is vaporized into vapor phase stream, and this vapor phase stream can be according to calibrating gas volume flow rate Q GasWith the knowledge of the density of its component and molecular weight and characterize.Liquid phase can alternatively be supplied by pre-atomized liquid stream, forms the drop spraying.Liquid or liquid spraying enter, and impact the surface that preheats in (11), and change over vapour phase from liquid phase, and this vapour phase is as materials flow (17) separating device of vaporization.In other embodiments, gas stream as the steam of liquid stream (16) or as diluent, can flow (16) access to plant together with liquid and leaves with the materials flow (17) of vaporization.Before access to plant during the vaporization cycle, be not regarded as Q for any material of gas LiquidOr Q GasA part, although in calculating dew point, must consider this material.In the second round of described device operation, may be at t dDelay period after begin, the materials flow of heating (14) is with volume flow rate Q RegenerationContinue for some time t through device Regeneration, an end of access to plant and leave in the opposite end as cool stream (15).This is to heat or regeneration step again.In the embodiment in figure 1, this materials flow is located access to plant (11) and is located to leave at entrance point (10) at the port of export (12).(not shown) in other embodiments, this materials flow can be located access to plant (11) and locates to leave at the port of export (12) in entrance point (10).
A key element of the present invention is, the vaporization of device with heat the cycle of operation again and share identical flow path.Recovery stream is heated to final higher temperature with described device from initial temperature (in one embodiment, the dew point of approximate reducible liquid charging), and this final higher temperature is higher than the dew point of liquid stream under the operating pressure of regulation.Be identified as T in this article Dew pointDew point, the temperature when being called as steam in the art and just having begun condensation, and depend on materials flow composition and pressure.This materials flow changes in a periodic manner, replaces between heat absorption vaporization stage (energy from the solid material to the liquid phase shifts) and heat release regeneration heat transfer stage (energy that flows to solid material from fluid shifts).According to materials flow condition (for example flow rate and speed), such as the combination of the thermophysical property of the geometrical factor of plant bulk and design and fluid and device, determine initial temperature and the final temperature of device.
The invention provides about the technical parameter of conduction flow through the geometry passages of vaporizer.This kind passage is restricted to by opening wide or " space " space that solid wall separates.In some embodiments of the present invention, wall itself can comprise some porositys that have usually much smaller than the aperture of 0.1mm.This kind porosity is not regarded as employed in this manual " space ", but only is regarded as the reducing of apparent density of solid wall.
The spatial variations of the geometric properties of device of the present invention and the size of voidage, voidage, comprise that the size and dimension of passage aisle feature of voidage is relevant.Along single imaginary space plane (19) as shown in fig. 1, local porosity is restricted to:
φ x = A ′ ( x ) A ( x ) .
Herein,
Figure BDA00003165165200052
Be the voidage at place, given locus, by subscript x indication, described device is A (x) at total cross-sectional area at this place, plane, and it is (x) given by A ' not comprise " opening wide " or " void area " of solid material in described plane.For the purposes of the present invention, we take following convention, have the flow axes from inlet surface (10) to exit surface (12), and " x " are the distances along this axis.Therefore, x is along the direction of vaporization flow (16), and locates to have null value in device import (10), and locates to have L in device outlet (12) AlwaysValue, wherein L AlwaysBe the device length of axis from import to outlet along fluid stream.We also adopt following convention: plane (19) are perpendicular to this flow axes.This kind plane is also referred to as " axial plane " in the art.Mean porosities or average void fraction along a certain length L of installing are restricted to:
φ a = ∫ 0 L A ′ ( x ) dx ∫ 0 L A ( x ) dx .
If average length L is taken as the total length L of described device Always, then
Figure BDA00003165165200062
Represent the average void fraction of whole device, be marked as
Figure BDA00003165165200063
If whole device occupies cumulative volume V Always(entity volume and porous volume), then total unlimited the or voidage in device is
Figure BDA00003165165200064
And the cumulative volume of the solid material in described device then is
Figure BDA00003165165200065
Figure BDA00003165165200066
We have found that the average void fraction of described device
Figure BDA00003165165200067
It is the parameter that makes this device successful operation.We have found that the average void fraction of allowing of apparatus of the present invention is 0.3 to 0.95.Preferably, the average void fraction of this device is 0.4 to 0.7.
In preferred embodiment, described voidage axially changes along the length of device.About the length of device, we refer to mainly along it dimension that steam flows take place.In Fig. 1, this dimension or direction are axial, herein by dimension or direction " x " indication.Be found preferably 0.5 to 0.995 in the surface void rate located of inlet surface (10) of device.Most preferred scope in this position is 0.65 to 0.995.In the voidage located of exit surface (12) of device preferably 0.2 to 0.7.The most preferred scope of outlet voidage is 0.35 to 0.6.
For the preferred embodiment that voidage wherein axially changes from the import to the exit surface, this variation can continuously changing or producing by a series of continuous constant voidages zones by voidage.Yet voidage changes, and the variation of voidage can be characterized as being the mean change on the whole length of device.For example, a group from import (10) to outlet (12)
Figure BDA00003165165200068
Value can be calculated by the least square method analysis that is known in the art
Figure BDA00003165165200069
Least square linear slope to x.This mean change can be expressed as slope or gradient (that is, the voidage of every length changes), or is expressed as average total void rate variation, and the latter is calculated as the least square slope and multiply by overall apparatus length (L Always).In many embodiments of the present invention, the variation of average total void rate is between 0.01 and 0.5.It is 0.15 to 0.35 that preferred average total void rate changes.We have found that the axial device average void fraction graded of permissible range is that every linear inch length 0.01 to 0.5 voidage descends.The preferred variation of average void fraction gradient is that every linear inch length 0.15 to 0.35 voidage descends.We have been found that also in the embodiment that uses a series of constant porosity region continuously therein, the quantity in preferred zone is greater than one and less than 20.The region quantity that is more preferably is two to ten, and most preferred quantity is two to five.
Described voidage is made of a lot of structurized small-sized void area, and wherein said structurized small-sized void area is identified as passage or passage area hereinafter.These passages form by simple shape and with the size of certain limit.The preferable shape that is used for the cross section of channel size void area is the shape of the rule of highly structural, for example circle, semicircle, annular, periodic wave wall ripple, or rectangular channel and groove.
An embodiment of described device is to have channel geometries almost identical on size and dimension in whole device volume.The preferred embodiment of this device is to have almost identical channel shape in device, has the size (that is the circular channel group that, has different-diameter) of variation in different axial positions.This device even embodiment that be more preferably has the axial variation of channel shape and size.In other words, changing shape and/or size can increase and can be used for the surface area that conducts heat and therefore can be used for vaporizing.
Optional embodiment has used the mixed and disorderly passage of the wormhole network that is made of millions of irregular channel shapes, and described irregular channel shape for example is the material characteristics of pottery or metal foam.Other embodiment has used by such as by the structure channel that piles up or the interleaving network of the wire rod that knit wire is made produces.
The channel shape of the void area of constituent apparatus can characterize with one group of Spatial Dimension.A dimension is called as hydraulic diameter.For the flow channel that is connected surface (that is, cylindrical, square, rectangle, triangle or bending channel) composition by simple sealed, hydraulic diameter is defined as d h=4A/P, wherein A is the cross-sectional area in the current-carrying space of passage, and P is the girth around confining surface.For not being the complex passages structure that is constituted by simple connection shape, can be according to relevant described axial plane with Fig. 1 (19) and the define channel hydraulic diameter.In any axial plane, d h' (x)=4A ' (x)/P ' (x), wherein A ' (x) represents total void area at given axial positions device, and P ' is the total length of the intersection surface between entity area and void area (x).
The characteristic level size h of described device FeatureCome rough estimate by getting device volume than the square root of total axial length, or
Figure BDA00003165165200081
We have been found that also some channel properties is preferred in the entry zone of device.The scope of this entry zone preferably device length about 5% and about 40% between.In other words, entry zone can be from x=0(inlet surface (10)) extend to x=0.05L at least AlwaysOr extend to x=0.4L at the most AlwaysPreferably, entry zone be device length 10% and 30% between.The direction of the passage in entry zone is arranged such that preferably the movement of the inlet flow stream introduced can be perpendicular to its mean flow direction.This allows to disperse blending ingredients and dispensing component to flow.Preferred design has and characteristic level size (h Feature) proportional flow path perpendicular to flow axes and axial direction following current.Preferably design the continuous-flow path that in entry zone, has perpendicular to flow axes, the characteristic level size (h that this continuous-flow path is described device Special Levy) at least 10% at the most 50%.Other preferably designs has L at least in all axial planes in the entry zone of described device AlwaysThe continuous-flow path of length.
We have found that, in described device entry zone, allow feature passage waterpower diameter d h(x) be 0.1 to 10mm, have 0.3 to 5mm preferred range and 0.7 to 2mm's even the scope that is more preferably.Feature channel size in this device exit is 0.2 to 5mm, has 0.4 to 2mm preferred range and 0.5 to 1.5mm's even the scope that is more preferably.
In preferred embodiment, the ratio of passage hydraulic diameter and passage length has at the preferred ratio between 10 and 5000 and between 40 and 200 even ratio that be more preferably between 0.5 and 10,000.
The further feature parameter of described device is the internal surface area that heats again that can be used for introducing the vaporization of stream and be used for the recuperator volume.The surface area of the per unit volume that we will measure in device partly is defined as S v=S/V, or the surface area of per unit volume, wherein S is included in the cumulative volume V(voidage+entity volume of regulation) interior interior surface area.An embodiment of the invention are used S vHomogeneity value.Optional embodiment of the present invention will use S in any zones of different of this device vNon-homogeneity value.The average S of this device vOnly be the device total surface area divided by the device cumulative volume, or S V, average=S Always/ V AlwaysWe have found that the internal surface area of the per unit volume of device allows that average range is at 10in 2/ in 3With 2000in 2/ in 3Between.The preferred value of the average range of the internal surface area of per unit volume is at 20in 2/ in 3With 1000in 2/ in 3Between.The average range of the internal surface area of per unit volume even value that be more preferably is at 50in 2/ in 3With 250in 2/ in 3Between.
Available heat transfer area and device volume have only been described at fluid and have been contacted with surface between the solid.Have been found that aspect heating efficiency, energy storage and energy transmission again, the composition of the solid material of described device and physical property it is successfully operated and effectively service ability will be helpful.Therefore, we have found that the composition that comprises the material of this device makes that the value of thermal capacity is 100J/kg-K at least, preferably be worth greater than 500J/kg, and even the thermal capacity value that is more preferably greater than 1000J/kg.
Consider that from aspect the heat management in device the thermo-contact between each zone of device should be maximized.We have found that the feasible value of the thermal conductivity of described material is 10W/m-K at least, preferably be worth greater than 50W/m-K, and the value that is more preferably is greater than 200W/m-K.We have been found that also the composition of the material that comprises described device makes that the density of solid material should be 2500kg/m at least 3, preferably be worth greater than 5000kg/m 3, and even the value that is more preferably greater than 7000kg/m 3
The particular design of described device will depend on to be finished the needed liquid injection condition of described vaporescence and time.Make the liquid stream of the special time period that flows vaporize required energy H by following formula
Provide:
Figure BDA00003165165200101
Figure BDA00003165165200108
Unit:
Figure BDA00003165165200104
In these expression formulas,
Figure BDA00003165165200105
Be the mass flowrate of liquid, λ LiquidBe the latent heat of vaporization in the liquid of mass unit, τ VaporizationBe the time period of injecting, Q VaporizationBe the normal volume specific gas flow rate of the liquid of vaporization, and λ VaporizationIt is the latent heat of vaporization in the liquid of calibrating gas volume unit.The vaporization energy of the speed of required energy and liquid supply, the per unit mass (or volume) of fluid and the duration of this process are proportional.Herein, the gaseous state of liquid base and conversion basis expression formula both is shown as the conversion factor that comprises them.The calibrating gas condition is well known in the art and gets usually 0 ℃ and 1 absolute atmosphere.
The energy storage available with it of the vaporization ability of described device is in direct ratio.The maximum temperature of this device will be the temperature when the liquid implantation step begins.This device mean temperature at this moment is T Dress Put the beginningWhen liquid is injected into and be vaporized, unit temp will drop to final mean temperature T Dress Put end, at this moment, the vaporization of operation cycle is partly finished.Herein, we are with Δ T DeviceBe defined as the liquid injection process mean temperature difference (T from start to end in device The device beginning-T Device eventually).The absolute value of high and low temperature will depend on the operating condition of device character and thermal balance and this process.The maximum vaporization capacity H ' of this device is provided by following formula:
Figure BDA00003165165200106
Unit:
Figure BDA00003165165200107
Herein, ρ DeviceBe the averag density of the solid material of device, φ is the mean porosities of device, C P, deviceBe the avergae specific heat capacity in the device of mass unit, and
Figure BDA00003165165200114
It is the avergae specific heat capacity in the device of volume unit
Figure BDA00003165165200112
The density of material of vaporization capacity and specific heat capacity, solid material volume and device is proportional, and in direct ratio with the temperature difference during process.
The normal volume that the air speed of system can be expressed as charging per hour gas flow rate is called as gas hourly space velocity divided by the volume of device, or GHSV.Gas feed speed is calculated as the mole rate of charging, and described material is considered as gaseous species, calculates with standard volume rate.For example, for the liquid implantation step, the liquid water charging that flows into 0.5 liter of device with the speed of 1g/ second has by the given gas hourly space velocity of following formula:
Figure BDA00003165165200113
Herein, Q VaporizationIt is normal volume gas flow rate (unit: NL/hr) and V AlwaysIt is the device cumulative volume.Generally speaking, according to per unit volume vaporization capacity speed, the miniaturization of described device and the efficient of generation and air speed are in direct ratio.For the integrated system of the hydrocarbon charging that utilizes experience subsequent chemistry or catalytic reaction, the whole air speed of system and the productivity of system are proportional.The expectation air speed has high as far as possible value.
Of the present invention preferred embodiment in, air speed GHSV is preferably more than 500, and even more preferably greater than 1000.
For the device with the circulation form operation, the heat that consumes in pervaporation step comes balance by the heat of storing in device during heating again (regeneration) part of circulation.If the liquid charging is supplied to two-forty (high GHSV), then heat is promptly exhausted, and must lack circulation timei.If the liquid charging is supplied to low rate (low GHSV), then heat is exhausted lentamente, and circulation timei is longer.Be arranged to equate in conjunction with the expression formula of above H and H ' and with them, provide following expression formula
Figure BDA00003165165200121
Be rewritten as in the nondimensional item of equation both sides and with this GHSV expression formula replacement expression formula above, provide following relation
Figure BDA00003165165200122
Herein, all variablees adopt their previous definition.
The heat transfer requirement of described device can be expressed as the product of the GHSV of the volume heat of vaporization of liquid charging and incoming flow.The volumetric heat transfer of vaporization requires:
Figure BDA00003165165200123
This is for the required energy transmission of the time per unit per unit volume of vaporizing liquid.Mention
Figure BDA00003165165200124
Expression formula be because hour but not second time dependence.These expression formulas define for gasifying liquid stream and have the necessary energy balance of abundant energy.
At liquid access to plant time period τ VaporizationAfterwards, make the stream of the heating again process device of heat the temperature rising is back to the initial high temperature when liquid injects the circulation beginning.This again during the heating period geometric properties of the ability of the temperature of raising device and device closely related, as earlier mentioned.Variable comprises the thermal property of porosity, hydraulic channel size and institute's constructing apparatus.Be known in the art, the porous media with feature channel passage shape that is made of solid material can characterize with heat transfer coefficient (h) and characteristic heat transfer surface area (A).Above define the preferred value of the surface area of per unit volume feature.Correlation based on the heat transfer coefficient of gas and solid property also is known in the art.These heat transfer coefficients are functions of the gentle phase composition of flow rate.Along with the feature channel size of porous material reduces, coefficient increases usually.Described volumetric heat transfer coefficient can be defined and provide with following unit
The volumetric heat transfer of the vaporization of rewriting with the chronomere of unanimity requires and can be written as
Figure BDA00003165165200132
Characteristic heat transfer temperature of the present invention requires to change with the ratio of the volumetric heat transfer coefficient that is used for device regeneration with the volume vaporization.This characteristic temperature difference is expressed as
ΔT HT＝H v/h v
This temperature difference has been described the balance between the heat transfer supply and demand during the cycling of device.As employed herein, this is based on employed heat transfer coefficient in the heating part again of circulation, described heating part more normally this circulation than the part of low heat transfer coefficient and with the design condition that is restricted.This temperature difference is the basic design parameters of device.Device design and the material character of requirement of the present invention satisfied in selection.
In practice of the present invention, feature Δ T HTPreferably between about 0.1 ℃ and 600 ℃.More preferably, feature Δ T HTShould be between 0.5 ℃ and 300 ℃.
The characteristic energy availability of described device is restricted to
Figure BDA00003165165200133
This is the preferred parameter for assessment of the validity of described device.Mean near one value the ideal of utilisable energy in vaporizer is used, and promptly shift the actual conditions of the required thermograde of heat less than 1.0 value reflection.We have found that the scope of required energy availability R is 0.05 to 0.7.Find preferably than R scope between 0.1 and 0.5.Most preferred scope is between 0.2 and 0.4.
The further feature of described device is low axial flow resistance in order to be minimized in that steam produces and the pressure drop during the thermal regeneration process again.For the orthotropy resistance, for example by the laminar flow of passage aisle, the axial flow resistance can be defined as:
Figure BDA00003165165200141
Unit: Δ p=[N/m 2(Pa)] ρ c=[hole slot/m 2] μ=[N second/m 2] GHSV=[hr -1] L=[m] d c=[m] φ x=[nothing]
Herein, Δ p is the pressure drop owing to frictional resistance, and L is mean space length, and dx is the local axial distance that increases, φ xBe local porosity, GHSV is gas hourly space velocity (unit: hr -1), μ is fluid viscosity, and ρ cBe hole slot (cell) the number concentration (quantity of the passage of described device per unit cross-sectional area) of per unit area.All values are regarded as the function of local coordinate, so that whole pressure drop is the overall contribution from all axial part of device.
Described pressure drop is subjected to number density, porosity and the GHSV(per unit volume flow of hole slot of channel size, the per unit area of auto levelizer) restriction.Porosity is relevant with channel size, and its expression formula is as follows:
d c 2 = 4 φ x π ρ c
Come the physical parameter of selecting arrangement in the mode of the design restriction of satisfying system operation.For those of ordinary skills, for the device of the wide dynamic range that is designed to operating condition, select design condition based on the maximum stream flow condition in the zone of the device with minimal flow passage.
The device characteristic of successful operation is that it is with low axial flow resistance operation, so that the overall average Δ p of described device per unit length is less than the 5psi/ inch.The parameter area allowable pressure drop that described device is allowed between 0.01 to 5psi/ inch, the pressure drop preferred range 0.03 and the 1psi/ inch between.
In one embodiment, can use the layout that is rolled into tight concentric ring or is stacked to the thin corrugated plate that closely separates the multiple metal composites in the layer to construct described device.This ripple geometry produces a series of circlet shape slotted eyes.Thickness by changing the rolled stock tablet and the density of wavy concentric ring or sheet and by change the encapsulation compactness along its axial length can change the diameter of slotted eye.
In an embodiment of this embodiment, described material is by Fecralloy
Figure BDA00003165165200151
The sheet of metal constitutes.For low voidage exit region cross section, select the ripple of this design and sheet thickness to be similar to 40% whole porosity (open volume) to produce.Low design porosity is used to satisfy the designing requirement (for thermal capacity and the energy storage under high flow rate condition) of maximum metal quality.The high porosity entry zone has approximate 80% porosity.This high porosity makes it possible to realize that the liquid of remarkable higher degree is penetrated in the internal volume of device.The inside of this device comprises the integral material of the median with about 60% porosity, and this integral material is used as the low porosity import of device and the transition part between the high porosity exit region.As earlier mentioned, described length of being made, and having change in the axial direction by continuous material pieces.
The porous design of described device makes it possible to provide the minimum pressure drop that flows from the fluid of supplying in either direction.Low pressure drop operation is specially adapted to following application, that is, this application relates to by the high speed that will cause droop loss significantly, high temperature gas flow heats device again.
Together with the heat release regenerative process, this device is useful especially for producing synthesis gas with circulation heat absorption steam reformation process.In reactor beds structure, use the electronic fuel injector to be injected into the mixture of liquid hydrocarbon fuel and liquid water on the surface, top (import) and be injected in the inner volume of vaporizer.Then, the downward gas coming through blender of the mixed flow of vaporization and flowing into subsequently in the reaction zone, in this reaction zone, charging is by using before the energy that had been stored in the bed from the heating part again of circulation to reform to the steam of synthesis gas.This synthesis gas flows out from device at the place, bottom, and can externally be utilized.
In the heating part again of this circulation, carbon monoxide, hydrogen and also may fuel mixture burned.Then, use this high-temperature stream to add the catalyst bed of thermal reaction area again.When the regeneration stage of this process finished, circulation was back to the liquid injection way.These two cyclic processes are equivalent to early to mention in this structure the present invention injects stage and heating period again.

Claims (21)

1. one kind is used for converting liquid feed stream to device that gas vapor flows, and described device comprises:
(a) have the channel component of first end and second end, described channel component has the passage of described first end of a plurality of connections and second end, and described channel component has roughly zone and the void area of entity,
(b) inlet member, described inlet member is used for described liquid feed stream is directed to first end of described a plurality of passages, and
(c) outlet member, described outlet member is used for guiding from the gas vapor stream of described a plurality of passages, the any distance d place of wherein said passage between described import and outlet has the geometry perpendicular to described feed flow direction, it is characterized in that: 1. void area A ' (x) and, 2. the total cross-sectional area A of passage (x), wherein the described void area A ' as the part of described gross area A (x) (x) is
Figure FDA00003165165100011
And along the average void fraction of length L of device
Described average void fraction is about 0.3 to about 0.95.
2. device according to claim 1, wherein, along the length of described device, described voidage is changed to about 0.2 to about 0.7 voidage at described outlet member place from about 0.5 to about 0.995 voidage in described inlet member.
3. device according to claim 2, wherein changing along the voidage of described device length is that every linear inch length about 0.01 to about 0.5 voidage descends.
4. device according to claim 3, wherein said variation is that every linear inch length about 0.15 to about 0.35 voidage descends.
5. device according to claim 1, wherein in quantity for greater than one and descend to described outlet member from described inlet member less than the described voidage in 20 the continuous constant voidage zone.
6. device according to claim 5, wherein the quantity in constant voidage zone is three to ten.
7. device according to claim 1, the feature of wherein said passage also is to have following passage waterpower diameter d H and passage length, described passage waterpower diameter d H be from described import department about 0.1 to about 10.0 millimeters in about 0.2 to about 0.5 of described exit.
8. device according to claim 7, wherein said passage hydraulic diameter be from described import department about 0.3 to about 5.0 millimeters to about 0.4 to about 2.0 millimeters of described exit.
9. device according to claim 7, wherein said passage hydraulic diameter is about 0.5 to about 10,000 with the ratio of passage length.
10. device according to claim 9, wherein said than being about 10 to about 5000.
11. device according to claim 10 is wherein said than being about 40 to about 200.
12. device according to claim 1, the feature of wherein said passage also are to have about 10in 2/ in 3To about 2000in 2/ in 3Average surface area per unit volume S V, average
13. device according to claim 12, wherein S V, averageBe about 20in 2/ in 3To about 1000in 2/ in 3
14. device according to claim 13, wherein S V, averageBe about 50in 2/ in 3To about 250in 2/ in 3
15. device according to claim 1, wherein said passage by thermal capacity at least 100J/Kg-K, thermal conductivity at least about 10W/m-K and density at least about 2500Kg/m 3Material make.
16. device according to claim 15, wherein said thermal capacity is at least about 500J/Kg, and thermal conductivity is at least about 50W/m-K, and density is at least about 5000Kg/m 3
17. device according to claim 16, wherein said thermal capacity is at least about 100J/Kg, and thermal conductivity is at least about 200W/m-K, and density is at least about 7000Kg/m 3
18. device according to claim 1, wherein said device moves under greater than about 500 gas hourly space velocity.
19. device according to claim 18, wherein said device moves under greater than about 1000 gas space velocity.
20. device according to claim 1, wherein said passage has the pressure drop less than about 5psi/ inch, Δ p.
21. device according to claim 20, wherein Δ p is less than about 1psi/ inch.
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